CN219355828U - Desulfurizing dust-removing device - Google Patents
Desulfurizing dust-removing device Download PDFInfo
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- CN219355828U CN219355828U CN202320121941.5U CN202320121941U CN219355828U CN 219355828 U CN219355828 U CN 219355828U CN 202320121941 U CN202320121941 U CN 202320121941U CN 219355828 U CN219355828 U CN 219355828U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
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Abstract
The utility model discloses a desulfurization dust removal device, which comprises an alkali recovery furnace, a dry dust remover, a circulating absorption reactor, a cloth bag dust remover and a chimney, wherein the alkali recovery furnace, the dry dust remover, the circulating absorption reactor and the cloth bag dust remover are arranged along the flow direction of flue gas purificationThe first outlet of the bag-type dust collector is connected with a chimney, the second outlet of the bag-type dust collector is connected with the inlet of the circulating absorption reactor, and the circulating absorption reactor is provided with a process water inlet, an absorbent inlet and a fly ash inlet. In the desulfurization dust removal device provided by the application, the flue gas of the alkaline furnace enters the dry dust remover through the flue after exiting the economizer, and the concentration of the discharged flue gas and dust is 50-100 mg/Nm after dust removal treatment 3 The viscosity of the desulfurization ash in the circulating absorption reactor is effectively reduced, namely, the viscosity of the desulfurization ash in the alkali recovery furnace is reduced, so that the stable circulating fluidization of the desulfurization ash is achieved.
Description
Technical Field
The utility model relates to the technical field of flue gas purification, in particular to a desulfurization dust removal device.
Background
In the paper industry, an alkali recovery furnace is a special boiler using concentrated black liquor of pulping waste liquor as fuel. The flue gas of the alkali recovery furnace is flue gas and water vapor generated by the combustion of black liquor sprayed into the combustion furnace.
Flue gas characteristics of the alkali recovery furnace: the flue gas of an alkali furnace is generally higher in moisture content, about 25%, and the higher the moisture content is, the higher the temperature of the flue gas is. The flue gas moisture content of the alkali furnace is mainly related to the concentration of black liquor entering the furnace, and the lower the concentration of black liquor entering the furnace is, the higher the flue gas moisture content is, otherwise, the higher the concentration of black liquor entering the furnace is, and the lower the flue gas moisture content is.
The treatment process of wet desulfurization, wet electricity, flue gas condenser, demister and SCR denitration is adopted, the treatment process is a wet flue gas treatment process of steel sintering, the process device is complex, the system process is long, the peripheral process is complex, the occupied area is large, and the operation and the running are inconvenient. Meanwhile, a large amount of wastewater is generated in the treatment process, the system has high corrosiveness, the control difficulty is high, and the maintenance workload is high. In addition, the device does not consider the high-viscosity sodium salt-rich dust in the flue gas of the alkali recovery boiler, and the dust can be adhered to a cooler and a demister in a large amount, so that the cooler and the demister are blocked, and the whitening effect is affected; at the same time, this dust may also adhere to subsequent SCR devices, resulting in catalyst failure poisoning.
Therefore, how to reduce the viscosity of the desulfurization ash of the alkali recovery furnace and achieve stable circulating fluidization of the desulfurization ash is a technical problem to be solved by the technicians in the field.
Disclosure of Invention
The utility model aims to provide a desulfurization dust removal device, which is used for reducing the viscosity of desulfurization ash of an alkali recovery furnace and achieving stable circulating fluidization of the desulfurization ash.
In order to achieve the above purpose, the utility model provides a desulfurization dust removal device, which comprises an alkali recovery furnace, a dry dust remover, a circulating absorption reactor, a cloth bag dust remover and a chimney, wherein the alkali recovery furnace, the dry dust remover, the circulating absorption reactor and the dust remover are sequentially arranged along the flow direction of flue gas purification, a first outlet of the dust remover is connected with the chimney, a second outlet of the dust remover is connected with an inlet of the circulating absorption reactor, and the circulating absorption reactor is provided with a process water inlet, an absorbent inlet and a fly ash inlet.
Optionally, in the desulfurization and dust removal device, an atomization nozzle connected with the process water inlet is arranged on the side part of the inner cavity of the circulating absorption reactor.
Optionally, in the desulfurization dust removal device, an inlet of the circulating absorption reactor is provided with a steady flow uniform distribution device for stabilizing air flow.
Optionally, in the desulfurization dust removal device, the flue gas desulfurization dust removal device further comprises a denitration device connected between the outlet of the bag-type dust collector and the inlet of the chimney along the flow direction of the flue gas.
Optionally, in the desulfurization dust removal device, the flue gas desulfurization dust removal device further comprises a first induced draft fan connected between the outlet of the denitration device and the inlet of the chimney along the flue gas flowing direction.
Optionally, in the desulfurization dust removal device, the desulfurization dust removal device further comprises a second induced draft fan connected between the outlet of the dry dust remover and the inlet of the circulating absorption reactor along the flow direction of the flue gas.
Optionally, in the desulfurization and dust removal device, the circulating absorption reactor is provided with a switching ash conveying device, the switching ash conveying device comprises a switching pneumatic gate valve, and the switching pneumatic gate valve conveys the fly ash to an inlet of the circulating reactor or a powder bin inlet.
Optionally, in the desulfurization dust-removing device, an absorbent adding device for adding absorbent to the circulating absorption reactor is further included, and the absorbent adding device is installed at the absorbent inlet.
Optionally, in the desulfurization dust removal device, the desulfurization dust removal device further comprises a process water spraying device for adding process water to the circulating absorption reactor, wherein the process water spraying device is arranged on the process water inlet.
Optionally, in the desulfurization dust collector, the dry dust collector is an electric dust collector or a cloth bag dust collector.
In the technical scheme, the desulfurization dust collector comprises an alkali recovery furnace, a dry dust collector, a circulating absorption reactor, a cloth bag dust collector and a chimney, wherein the alkali recovery furnace, the dry dust collector, the circulating absorption reactor and the dust collector are sequentially arranged along the flow direction of flue gas purification, a first outlet of the dust collector is connected with the chimney, a second outlet of the dust collector is connected with an inlet of the circulating absorption reactor, and the circulating absorption reactor is provided with a process water inlet, an absorbent inlet and a fly ash inlet.
According to the above description, in the desulfurization dust removal device provided by the application, the flue gas of the alkaline furnace enters the dry dust remover through the flue after exiting the economizer, and the flue gas and dust are concentrated after dust removal treatmentThe degree is 50-100 mg/Nm 3 . Fresh calcium-based absorbent and process water are arranged at the inlet of the circulating absorption reactor, and fly ash is added at the same time, so that large particles formed by the functions of condensation and granulation after the circulating absorption reactor are easily captured by a rear-end bag-type dust collector, and the dust emission concentration is less than 10mg/Nm 3 The natural white ash adding mixed formula is formed, so that the viscosity of the desulfurized ash in the circulating absorption reactor is effectively reduced, namely the viscosity of the desulfurized ash in the alkali recovery furnace is reduced, and stable circulating fluidization of the desulfurized ash is achieved.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are required to be used in the embodiments or the description of the prior art will be briefly described below, and it is obvious that the drawings in the following description are only embodiments of the present utility model, and that other drawings can be obtained according to the provided drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of a desulfurizing and dedusting apparatus according to an embodiment of the present utility model.
Wherein in fig. 1: 1-alkali recovery furnace, 2-dry dust collector, 3-circulating absorption reactor, 4-cloth bag dust collector, 5-denitration device and 6-chimney.
Detailed Description
The utility model aims at providing a desulfurization dust removal device to reduce the viscosity of desulfurization ash of an alkali recovery furnace and achieve stable circulating fluidization of the desulfurization ash.
The present utility model will be described in further detail below with reference to the drawings and embodiments, so that those skilled in the art can better understand the technical solutions of the present utility model.
Please refer to fig. 1.
In a specific implementation manner, the desulfurization dust removal device provided by the specific embodiment of the utility model comprises an alkali recovery furnace 1, a dry dust remover 2, a circulating absorption reactor 3, a bag-type dust remover 4 and a chimney 6, wherein the alkali recovery furnace 1, the dry dust remover 2, the circulating absorption reactor 3 and the dust remover are sequentially arranged along the flow direction of flue gas purification, and the dust remover is arranged in sequenceThe first outlet is connected with a chimney 6, the second outlet of the dust remover is connected with the inlet of the circulating absorption reactor 3, and the circulating absorption reactor 3 is provided with a process water inlet, an absorbent inlet and a fly ash inlet. In one embodiment, the absorbent is CaO, ca (OH) and is added through the absorbent inlet 2 Calcium-based absorbents. The quality of the absorbent is as follows: the CaO content is more than or equal to 85 percent; the grain diameter is less than or equal to 1mm; t (T) 60 ≤4min。
Specifically, the dry dust collector 2 is an electric dust collector, a cloth bag dust collector or other dust collecting equipment.
Flue gas of the alkali recovery furnace 1 enters a dry dust remover 2 through a flue, and after dust removal treatment, the concentration of the discharged flue gas and dust is 50-100 mg/Nm 3 . Adopting a dry dust remover 2+ circulating absorption reactor 3+ cloth bag dust remover 4 to absorb and remove SO 2 、SO 3 、HCl、HF、H 2 S and other pollutants and capturing high-viscosity sodium salt-rich dust.
In order to improve the dust removal treatment effect, preferably, the circulating absorption reactor 3 sprays the process water through an atomization nozzle, and specifically, the atomization nozzle is arranged at the side end of the inner cavity of the circulating absorption reactor 3 and is connected with a process water inlet. The number of the atomizing nozzles can be one or two, and preferably, the atomizing nozzles are arranged in an array.
In one specific embodiment, the inlet of the circulating absorption reactor 3 is provided with a steady flow uniform distribution device. The dust-removed circulating absorption reactor 3, high-pressure atomization process water is sprayed into the circulating absorption reactor 3 for humidification, the temperature of the flue gas is controlled between 100 ℃ and 130 ℃, SO that an ionic reaction environment is formed in the circulating absorption reactor 3, and SO in the flue gas 2 、SO 3 、HCl、HF、H 2 S and other pollutants react with the added fresh absorbent and the recycled materials quickly and are removed. In the circulating absorption reactor 3, the Ca/S ratio of the fresh absorbent is controlled between 1.2 and 1.6, the pressure drop of a material bed layer is 1.2 to 1.4kPa, the diameter and the height of the circulating absorption reactor 3 meet the requirement of 5 to 8S of flue gas reaction time, and a steady flow uniform distribution device is arranged at the inlet of the circulating absorption reactor 3, so that the flue gas entering the circulating absorption reactor 3 is uniformly distributed, and the pollutants in the flue gas and the calcium-based absorbent are fully mixedContact, reaction enhancement and SO realization 3 、HCl、HF、H 2 S and the like are basically and completely removed, SO 2 The discharge concentration was reduced to 35mg/Nm 3 Within the inner part.
In one embodiment, the fly ash inlet position is provided with a switching ash conveying device, and the switching ash conveying device comprises a pneumatic gate valve, and the pneumatic gate valve conveys the fly ash to the circulating reactor 3. Of course, fly ash can also be conveyed to other bins by switching the outlet of the pneumatic gate valve.
In one embodiment, the desulfurization dust-removing device further comprises an absorbent adding device for adding absorbent to the circulating absorption reactor 3, wherein the absorbent adding device is arranged at the absorbent inlet, and specifically, the absorbent can be added to the circulating absorption reactor 3 by controlling the absorbent adding device. The desulfurization and dust removal device further comprises a process water spraying device for adding process water into the circulating absorption reactor 3, and specifically, the process water spraying device can be a spraying device for spraying high-pressure atomized process water, and the process water spraying device is arranged on the process water inlet. The utility model provides a be equipped with absorbent feeding device, process water spraying device (be used for adding process water to circulating absorption reactor 3) and switch ash conveying device of fresh calcium-based absorbent at circulating absorption reactor 3 entry, according to SO in the flue gas 2 The concentration is adjusted to control the adding amount of the fresh calcium-based absorbent, the Ca/S ratio of the added fresh calcium-based absorbent is 1.2-1.6, the pressure drop of the bed layer in the circulating absorption reactor 3 is 1.2-1.4 kPa, the reaction temperature is 100-130 ℃, and the diameter and the height of the circulating absorption reactor 3 meet the reaction time of the flue gas of 5-8S.
Because the high-viscosity sodium salt-rich dust is adsorbed and wrapped by materials in the circulating reaction environment of high humidity and high turbulence in the circulating absorption reactor 3, the dust is coagulated and aggregated to form larger particles. The rear end of the circulating absorption reactor 3 is connected with a cloth bag dust remover 4, and the large particles formed by condensation are easily removed by the cloth bag dust remover 4 at the rear end, so that the dust concentration discharge at the outlet of the cloth bag dust remover 4 is less than 10mg/Nm 3 . After passing through the circulating absorption reactor 3, the flue gas temperature is 100-130 ℃, SO that SO is realized 3 、HCl、HF、H 2 S and other pollutants are completely removed to realize SO 2 The discharge concentration is less than 35mg/Nm 3 And the high-viscosity sodium salt-rich dust in the flue gas is adsorbed and wrapped by materials in the circulating absorption reactor 3 to form larger particles which are easy to be removed by the rear-end bag-type dust collector 4, so that the dust emission concentration is less than 10mg/Nm 3 。
Most of the materials in the bag-type dust collector 4 can be returned to the circulating absorption reactor 3 through the air circulating chute to continue to participate in the reaction, and a small amount of reacted waste is conveyed to a waste storage bin through the discharging chute and the bin pump conveying system and finally conveyed away through a sealed tank car or other transport vehicles.
The circulating absorption reactor 3 is internally provided with high-viscosity sodium salt-rich dust, and the material property in the circulating absorption reactor 3 is changed and the viscosity is enhanced through water spraying, cooling and repeated circulating absorption. Therefore, the fly ash of the boiler of the thermal power plant in the factory of the papermaking industry is periodically and stage-by-stage conveyed into the circulating absorption reactor 3 by the linkage control of the double-switching ash conveying system, so that a natural white ash adding mixed formula is formed, the viscosity of the desulfurized ash in the circulating absorption reactor 3 is effectively reduced, and the circulation of materials and the discharge conveying and treatment of waste materials are facilitated.
In a specific embodiment, if NOx in the flue gas needs to be further removed, the outlet of the bag-type dust collector 4 can be selectively connected with a denitration system device of the SCR. After the alkali furnace flue gas is treated by the front-end circulating absorption reactor 3+ cloth bag dust remover 4, the high-viscosity sodium salt-rich dust in the flue gas is removed, so that the high-viscosity dust cannot appear in the subsequent denitration device 5, the good reaction environment of the catalyst is ensured, and the stable operation of a denitration system is further ensured. And finally, the flue gas is discharged to a chimney 6 through an induced draft fan, so that the stable operation of the denitration system is further ensured.
In order to facilitate stable flow of the flue gas, preferably, the desulfurization and dust removal device further comprises a first induced draft fan connected between the outlet of the denitration device 5 and the inlet of the chimney 6 along the flow direction of the flue gas.
In order to improve the working efficiency, the desulfurization dust-removing device preferably further comprises a second induced draft fan connected between the outlet of the dry dust collector 2 and the inlet of the circulating absorption reactor 3 along the flow direction of the flue gas.
In a specific embodiment, the alkali recovery furnace 1 with a rated black liquor solids handling capacity of 900tds/d has an exhaust gas flow of 270000Nm after exiting the economizer of the alkali recovery furnace 1 3 And/h, the flue gas temperature of the coal outlet economizer of the alkali recovery furnace 1 is 175 ℃, and the flue gas SO of the coal outlet economizer of the alkali recovery furnace 1 2 The concentration was 200mg/Nm 3 The flue gas and dust concentration of the coal outlet device of the alkali recovery furnace 1 is 10-30 g/Nm 3 Meets the dust concentration of the outlet of a chimney 6<10mg/Nm 3 ，SO 2 Concentration of<35mg/Nm 3 Is required by the ultra-low emission standard.
The parameters of the front-end dry dust collector 2 are set as follows:
flue gas of the alkali recovery furnace 1 enters a front-end dry dust remover 2 through a flue, the dry dust remover 2 can be an electric dust remover or a cloth bag dust remover 4, and the concentration of the discharged flue gas and dust is 50-100 mg/Nm after dust removal treatment 3 。
The parameters of the cyclic absorption reactor 3 were set as follows:
1. the flue gas to be purified enters the circulating absorption reactor 3 from the front-end dust remover through a second induced draft fan, fresh absorbent is added into the circulating absorption reactor 3, high-pressure atomization process water is sprayed in, the reaction temperature is 100-130 ℃, the bed pressure drop is 1.2-1.4 kPa, and the reaction time is 5-8S. The concentration of SO2 in the flue gas is reduced from 200mg/Nm3 to below 35mg/Nm3, SO that the high-efficiency removal of SO2 is realized, other pollutants such as SO3, HCl, HF, H2S and the like are basically and completely removed, and the high-viscosity sodium salt-rich dust in the flue gas is adsorbed and wrapped by materials in the circulating absorption reactor 3, and is condensed and aggregated to form larger particles.
2. The linkage control of the double-switching ash conveying system is adopted, the boiler fly ash of the thermal power plant is periodically conveyed to the circulating absorption reactor 3 in stages, a natural white ash adding mixed formula is formed, and the viscosity of the desulfurized ash in the circulating absorption reactor 3 is effectively reduced.
3. After passing through the circulating absorption reactor 3, the dust concentration in the flue gas reaches 800-1000 g/Nm3, and then enters into the special efficient cloth for rear-end dry desulfurizationThe bag dust collector 4 is used for realizing that the formed larger particles are easy to be caught by the rear-end bag dust collector 4 due to the functions of condensation and granulation after the circulating absorption reactor 3, so that the dust emission concentration is less than 10mg/Nm 3 。
Reaching SO 2 Ultra low emission of dust (SO 2 Concentration of<35mg/Nm 3 Dust, dust<10mg/Nm 3 )。
In the circulating absorption reactor 3, the flue gas fully reacts with the added fresh absorbent and the circulating desulfurization ash to realize SO 2 The high-viscosity sodium salt-rich dust in the flue gas is efficiently adsorbed, and the high-content water in the flue gas can be effectively evaporated under the turbulent action of the high-density materials. Finally, the flue gas with high humidity and high viscosity dust concentration passes through the high-efficiency bag-type dust collector 4, so that the ultra-low emission of dust is realized.
According to the utility model, the natural white ash adding formula of the boiler fly ash of the thermal power plant and the flue gas desulfurization ash of the alkali recovery furnace 1 in the factory of the papermaking industry is utilized, the desulfurization ash replacement is carried out through the linkage control of the double-switching ash conveying system, the viscosity of the desulfurization ash of the alkali recovery furnace 1 is reduced, and the purpose of stable circulating fluidization of the desulfurization ash is achieved.
The whole system has no waste water generation, no corrosion, simple and compact operation, compact equipment, small occupied area and lower investment and operation cost, so that the flue gas of the alkali recovery furnace 1 is purified. Meanwhile, the natural white ash adding formula of the fly ash of the heat power plant boiler and the flue gas desulfurization ash of the alkali recovery furnace 1 in the factory of the papermaking industry is utilized, the desulfurization ash replacement is carried out through the linkage control of the double-switching ash conveying system, the viscosity of the desulfurization ash of the alkali recovery furnace 1 is reduced, and the method can be well suitable for the high-viscosity sodium salt-rich dust characteristics in the flue gas of the alkali recovery furnace 1. Can adapt to the characteristic of high-viscosity dust in the flue gas of the alkali recovery furnace 1, and realize the circulation of materials and the discharge and the transportation of waste materials.
In the present specification, each embodiment is described in a progressive manner, and each embodiment is mainly described in a different point from other embodiments, and identical and similar parts between the embodiments are all enough to refer to each other.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present utility model. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present utility model is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. The utility model provides a desulfurization dust collector, its characterized in that includes alkali recovery stove (1), dry dust remover (2), circulation absorption reactor (3), sack cleaner (4) and chimney (6), along flue gas purification flow direction, alkali recovery stove (1) dry dust remover (2) circulation absorption reactor (3) and dust remover are arranged in proper order, dust remover first exit linkage chimney (6), the second exit linkage of dust remover the import of circulation absorption reactor (3), circulation absorption reactor (3) are equipped with technology water import, absorbent import and fly ash import.
2. The desulfurization and dust removal device according to claim 1, characterized in that an atomizer connected with the process water inlet is provided at the side of the inner cavity of the circulating absorption reactor (3).
3. The desulfurization and dust removal device according to claim 1, wherein the inlet of the circulating absorption reactor (3) is provided with a steady flow uniform distribution device for stabilizing the air flow.
4. The desulfurization and dust-removal device according to claim 1, further comprising a denitrification device (5) connected between the outlet of the bag-type dust collector (4) and the inlet of the chimney (6) in the flow direction of flue gas.
5. The desulfurization and dust-removal device according to claim 4, further comprising a first induced draft fan connected between the outlet of the denitration device (5) and the inlet of the chimney (6) in the flue gas flow direction.
6. The desulfurization dust-removing device according to claim 1, further comprising a second induced draft fan connected between the outlet of the dry dust collector (2) and the inlet of the circulating absorption reactor (3) in the flow direction of flue gas.
7. The desulfurization and dust-removing device according to claim 1, characterized in that the fly ash inlet position is provided with a switching ash-conveying device, which comprises a pneumatic gate valve, which conveys fly ash to the circulating absorption reactor (3).
8. The desulfurization dust-removing device according to claim 1, further comprising an absorbent adding device for adding an absorbent to the circulating absorption reactor (3), said absorbent adding device being installed at the absorbent inlet.
9. The desulfurization and dust-removing device according to claim 1, further comprising a process water injection device for adding process water to the circulating absorption reactor (3), the process water injection device being installed on the process water inlet.
10. The desulfurization dust-removing device according to any one of claims 1-9, characterized in that the dry dust collector (2) is an electric dust collector or a bag-type dust collector.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320121941.5U CN219355828U (en) | 2023-01-16 | 2023-01-16 | Desulfurizing dust-removing device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320121941.5U CN219355828U (en) | 2023-01-16 | 2023-01-16 | Desulfurizing dust-removing device |
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| CN219355828U true CN219355828U (en) | 2023-07-18 |
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| CN202320121941.5U Active CN219355828U (en) | 2023-01-16 | 2023-01-16 | Desulfurizing dust-removing device |
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